Method of estimating hydrocarbon storage in a catalytic device

ABSTRACT

A method of estimating hydrocarbon storage in a catalytic device of an exhaust gas treatment system includes calculating an amount of hydrocarbons absorbed in the catalytic device per unit volume of exhaust gas over a period of time, calculating an amount of hydrocarbons desorbed in the catalytic device per unit volume of exhaust gas over the period of time, and calculating an amount of hydrocarbons oxidized in the catalytic device per unit volume of exhaust gas over the period of time. The amount of hydrocarbons oxidized in the catalytic device and the amount of hydrocarbons desorbed in the catalytic device are subtracted from the amount of hydrocarbons absorbed in the catalytic device to determine the amount of hydrocarbons stored in the catalytic device.

TECHNICAL FIELD

The invention generally relates to a method of estimating a quantity ormass of hydrocarbon storage in a catalytic device of an exhaust gastreatment system.

BACKGROUND

Vehicles with an Internal Combustion Engine (ICE) include an exhaust gastreatment system for reducing the toxicity of the exhaust gas from theengine. The treatment system typically includes at least one and oftenmultiple catalytic devices. If the engine includes a diesel engine, thenthe catalytic devices may include, for example, one or more of a dieselparticulate filter, a diesel oxidation catalyst, a catalytic converter,and/or a selective catalytic reduction device. Each of the catalyticdevices includes a catalyst that reduces nitrogen oxides in the exhaustgas to nitrogen and carbon dioxide or water, as well as oxidizes carbonmonoxide (CO) and unburnt hydrocarbons (HCs) to carbon dioxide andwater. The catalyst may include, but is not limited to, Platinum GroupMetals (PGM). The catalyst must be heated to a light-off temperature ofthe catalyst before the catalyst becomes operational. Accordingly, theexhaust gas must heat the catalyst to the light-off temperature beforethe reaction between the catalyst and the exhaust gas begins. Thecatalyst may be intentionally heated to the light-off temperature duringa regeneration process to burn off the accumulated hydrocarbons.

In order to determine when to regenerate the exhaust gas treatmentsystem, the vehicle may use a model to predict when the catalyticdevice(s) are required to be regenerated. The model provides anestimation of the accumulated hydrocarbons in the catalytic device,based on one or more actual operating conditions of the vehicle. Theoperation of the engine may be controlled to heat the catalyst to thelight-off temperature, to regenerate the catalytic device(s), based onthe estimated hydrocarbon accumulation or storage from the model.

SUMMARY

A method of estimating hydrocarbon storage in a catalytic device of anexhaust gas treatment system is provided. The method includescalculating an amount of hydrocarbons absorbed in the catalytic deviceper unit volume of exhaust gas over a period of time, calculating anamount of hydrocarbons desorbed in the catalytic device per unit volumeof exhaust gas over the period of time, and calculating an amount ofhydrocarbons oxidized in the catalytic device per unit volume of exhaustgas over the period of time. The amount of hydrocarbons oxidized in thecatalytic device and the amount of hydrocarbons desorbed in thecatalytic device are subtracted from the amount of hydrocarbons absorbedin the catalytic device to determine the amount of hydrocarbons storedin the catalytic device. The exhaust gas treatment system is thencontrolled based upon the estimated hydrocarbon storage of the catalyticdevice.

A method of estimating hydrocarbon storage in a catalytic device of anexhaust gas treatment system is also provided. The method includesestimating the hydrocarbon storage of the catalytic device from Equation1)

$\begin{matrix}{{\Omega \frac{\theta_{HC}}{t}} = {\frac{{\Delta \lbrack{HC}\rbrack}_{absorp} - {\Delta \lbrack{HC}\rbrack}_{desorp} - {\Delta \lbrack{HC}\rbrack}_{oxi}}{\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}.}} & \left. 1 \right)\end{matrix}$

Referring to Equation 1 above,

$\Omega \frac{\theta_{HC}}{t}$

is the rate of change in hydrocarbon storage per unit volume of thecatalytic device, Δ[HC]_(absorp) is the amount of hydrocarbons absorbedin the catalytic device per unit volume of exhaust gas, Δ[HC]_(desorp)is the amount of hydrocarbons desorbed in the catalytic device per unitvolume of exhaust gas, Δ[HC]_(oxi) is the amount of hydrocarbonsoxidized in the catalytic device per unit volume of exhaust gas, t_(res)is the residence time of the exhaust gas within the catalytic device,and Δt is the change in time (i.e., time duration). The exhaust gastreatment system is then controlled based upon the estimated hydrocarbonstorage of the catalytic device.

Accordingly, Equation 1 is a mass balance equation that balances theincoming mass of the hydrocarbons with the outgoing mass of thehydrocarbons to estimate that the amount of hydrocarbons stored in thecatalytic device.

The above features and advantages and other features and advantages ofthe present invention are readily apparent from the following detaileddescription of the best modes for carrying out the invention when takenin connection with the accompanying drawings.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a flowchart showing a method of estimating hydrocarbon storagein a catalytic device.

FIG. 2 is a schematic diagram showing a mapping structure fordetermining a normalized hydrocarbon storage desorption rate(k_(desorp)).

FIG. 3 is a schematic diagram showing a mapping structure fordetermining an amount of hydrocarbons absorbed in the catalytic deviceper unit volume of exhaust gas (Δ[HC]_(absorp)).

FIG. 4 is a schematic diagram showing a mapping structure fordetermining an amount of O2 (oxygen) consumed in the catalytic deviceper unit volume of exhaust gas (Δ[O2]).

DETAILED DESCRIPTION

Those having ordinary skill in the art will recognize that terms such as“above,” “below,” “upward,” “downward,” “top,” “bottom,” etc., are useddescriptively for the figures, and do not represent limitations on thescope of the invention, as defined by the appended claims. Furthermore,the invention may be described herein in terms of functional and/orlogical block components and/or various processing steps. It should berealized that such block components may be comprised of any number ofhardware, software, and/or firmware components configured to perform thespecified functions.

Referring to the Figures, wherein like numerals indicate like partsthroughout the several views, a flowchart showing a method of estimatinghydrocarbon storage in a catalytic device of an exhaust gas treatmentsystem is generally shown in FIG. 1. As is generally appreciated, theexhaust gas treatment system treats the flow of exhaust gas from anengine, such as but not limited to a diesel engine or a gasoline engine.The exhaust gas treatment system may include one or more devices thatinclude a catalyst, such as but not limited to a catalytic converter.When the engine is a diesel engine, the catalytic device may include,but is not limited to, a diesel oxidation catalyst, a diesel particulatefilter, or a selective catalytic reduction system. In order to properlycontrol the catalytic device, a vehicle controller must estimate theamount of hydrocarbon storage of the catalytic device. For example, thecontroller may use the estimated amount of hydrocarbon storage of thecatalytic device to determine when to regenerate, i.e., burn off, thehydrocarbons stored in the catalytic device.

As noted above, the vehicle includes a controller to control and/ormonitor the operation of the engine and/or an exhaust gas treatmentsystem, including the catalytic device. The controller may include acomputer and/or processor, and include all software, hardware, memory,algorithms, connections, sensors, etc., necessary to manage, monitor,and control the operation of the engine and the exhaust gas treatmentsystem. As such, the method described below may be embodied as a programoperable on the controller. It should be appreciated that the controllermay include any device capable of analyzing data from various sensors,comparing data, making the necessary decisions required to control theoperation of the engine and/or exhaust gas treatment system, and performthe various calculations required to calculate the estimated hydrocarbonstorage of the catalytic device.

Referring to FIG. 1, the method of estimating the amount of hydrocarbonstorage in the catalytic device includes calculating an amount ofhydrocarbons absorbed in the catalytic device per unit volume of exhaustgas over a period of time, generally indicated by box 20, calculating anamount of hydrocarbons desorbed in the catalytic device per unit volumeof exhaust gas over the period of time, generally indicated by box 22,and calculating an amount of hydrocarbons oxidized in the catalyticdevice per unit volume of exhaust gas over the period of time, generallyindicated by box 26. The amount of hydrocarbons oxidized 26 in thecatalytic device and the amount of hydrocarbons desorbed 22 in thecatalytic device are subtracted from the amount of hydrocarbons absorbed20 in the catalytic device, generally indicated by box 28, to determinethe amount of hydrocarbons stored in the catalytic device, generallyindicated by box 30. Accordingly, the method uses a mass balance betweenthe hydrocarbon absorption 20, hydrocarbon desorption 22, andhydrocarbon oxidation 26 to determine the hydrocarbon storage of thecatalytic device.

The hydrocarbon storage of the catalytic device may be estimated fromEquation 1:

$\begin{matrix}{{{\Omega \frac{\theta_{HC}}{t}} = \frac{{\Delta \lbrack{HC}\rbrack}_{absorp} - {\Delta \lbrack{HC}\rbrack}_{desorp} - {\Delta \lbrack{HC}\rbrack}_{oxi}}{\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}};} & \left. 1 \right)\end{matrix}$

wherein

$\Omega \frac{\theta_{HC}}{t}$

is the rate of change in hydrocarbon storage per unit volume of thecatalytic device, Δ[HC]_(absorp) is the amount of hydrocarbons absorbedin the catalytic device per unit volume of exhaust gas, Δ[HC]_(desorp)is the amount of hydrocarbons desorbed in the catalytic device per unitvolume of exhaust gas, Δ[HC]_(oxi) is the amount of hydrocarbonsoxidized in the catalytic device per unit volume of exhaust gas, t_(res)is the residence time of the exhaust gas within the catalytic device,and Δt is the change in time (i.e., time duration).

The amount of hydrocarbons desorbed in the catalytic device per unitvolume (Δ[HC]_(desorp)) may be calculated from Equation 2:

$\begin{matrix}{{\Delta \lbrack{HC}\rbrack}_{desorp} = {\left( \frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}} \right)\Omega \; k_{desorp}}} & \left. 2 \right)\end{matrix}$

wherein t_(res) is the residence time of the exhaust gas within thecatalytic device, Δt is the change in time (i.e., time duration), Ω isthe maximum amount of hydrocarbon storage per unit volume of thecatalytic device, and k_(desorp) is the normalized hydrocarbon storagedesorption rate.

Referring to FIG. 2, a value for the normalized hydrocarbon storagedesorption rate (k_(desorp)), generally indicated by box 32, may beobtained from a desorption rate table 34, stored in the memory of thecontroller. Obtaining the normalized hydrocarbon storage desorptionrate, generally indicated by box 36, which is used to calculate theamount of hydrocarbons desorbed in the catalytic device per unit volume(Δ[HC]_(desorp)), may include referencing the desorption rate table 34to look up the normalized hydrocarbon storage desorption rate(k_(desorp)) 32. The desorption rate table 34 may be defined as a twodimensional table, that uses two input values to define an output value.The normalized hydrocarbon storage desorption rate (k_(desorp)) 32 isbased upon a temperature of the catalytic device (T) 38, and anormalized hydrocarbon storage of the catalytic device (θ_(HC)) 40.Accordingly, the controller may use the temperature of the catalyticdevice (T) 38 and a normalized hydrocarbon storage of the catalyticdevice (θ_(HC)) 40 as the two inputs into the desorption rate table 34,to look up and/or define the value for the normalized hydrocarbonstorage desorption rate (k_(desorp)) 32, which is the output of thedesorption rate table.

The amount of hydrocarbons oxidized in the catalytic device per unitvolume of exhaust gas (Δ[HC]_(oxi)) may be calculated from Equation 3:

$\begin{matrix}{{{\Delta \lbrack{HC}\rbrack}_{oxi} = \frac{\Delta \left\lbrack {O\; 2} \right\rbrack}{{Ratio}_{{{stoic}\_ O}\; 2{\_ {HC}}}}};} & \left. 3 \right)\end{matrix}$

wherein Δ[O2] is the O2 (oxygen) consumed in the catalytic device perunit volume of exhaust gas, and Ratio_(stoic) _(—) _(O2) _(—) _(HC) isthe O2 and hydrocarbon reaction stoichiometric ratio.

Referring to FIG. 3, the O2 consumed in the catalytic device per unitvolume of exhaust gas 44 (Δ[O2]) is a function of an oxygen burnefficiency ratio 46 and an amount of O2 available for reaction withhydrocarbons per unit volume of exhaust gas 48. The amount of O2available for reaction with hydrocarbons per unit volume of exhaust gas48 may be calculated from Equation 4:

$\begin{matrix}{{\eta_{diff}\left( \frac{\left\lbrack {O\; 2} \right\rbrack_{in} + {\left\lbrack {O\; 2} \right\rbrack_{- 1}\frac{t_{res}}{\Delta \; t}}}{1 + \frac{t_{res}}{\Delta \; t}} \right)};} & \left. 4 \right)\end{matrix}$

wherein η_(diff) is the oxidation catalyst diffusion efficiency ratio,[O2]_(in) is the oxidation catalyst inlet O2 concentration, [O2]⁻¹ isthe O2 concentration in the catalytic device at a last time increment,t_(res) is the residence time of the exhaust gas within the catalyticdevice, and Δt is the change in time (i.e., time duration).

As shown in FIG. 3, a value for the oxygen burn efficiency ratio 46 maybe obtained from a burn efficiency table 50, stored in the memory of thecontroller. Obtaining the value, generally indicated by box 52, for theoxygen burn efficiency ratio 46, which is used to calculate the O2consumed in the catalytic device per unit volume of exhaust gas 44(Δ[O2]), may include referencing the burn efficiency table 50 to look-upthe value for the oxygen burn efficiency ratio 46. The burn efficiencytable 50 may be defined as a two dimensional table, that uses two inputvalues to define an output value. The oxygen burn efficiency ratio 46 isbased upon a temperature of the catalytic device 38 (T), and a firstintermediate variable for hydrocarbon oxidation 54. Accordingly, thecontroller may use the temperature of the catalytic device 38 (T) andfirst intermediate variable for hydrocarbon oxidation 54 as the twoinputs into the burn efficiency table 50, to look up and/or define thevalue for the oxygen burn efficiency ratio 46, which is the output ofthe burn efficiency table 50.

As shown in FIG. 3, the first intermediate variable for hydrocarbonoxidation 54 is a function of a second intermediate variable forhydrocarbon oxidation 56 (ζ_(O2)), and an oxidation catalyst diffusionefficiency ratio 58. The second intermediate variable for hydrocarbonoxidation 56 (ζ_(O2)) may be calculated from Equation 5:

$\begin{matrix}{{\varsigma \; O\; 2} = {\Omega \; {f\left( \theta_{HC} \right)}\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}} & \left. 5 \right)\end{matrix}$

wherein Ω is the maximum amount of hydrocarbon storage per unit volumeof the catalytic device, ƒ(θ_(HC)) is a function of the normalizedhydrocarbon storage of the catalytic device, t_(res) is the residencetime of the exhaust gas within the catalytic device, and Δt is thechange in time (i.e., time duration).

As shown in FIG. 3, a value for the oxidation catalyst diffusionefficiency ratio 58 may be obtained from a diffusion efficiency table60, stored in the memory of the controller. Obtaining the value,generally indicated by box 62, for the oxidation catalyst diffusionefficiency ratio 58, which is used to calculate the first intermediatevariable for hydrocarbon oxidation 54, may include referencing thediffusion efficiency table 60 to look-up the value for the oxidationcatalyst diffusion efficiency ratio 58. The diffusion efficiency tablemay be defined as a one dimensional table that uses one input value todefine a single output value. The oxidation catalyst diffusionefficiency ratio 58 is based upon a residence time of the exhaust gaswithin the catalytic device 64 (t_(res)). Accordingly, the controllermay use the residence time of the exhaust gas within the catalyticdevice 64 (t_(res)) as the single input into the diffusion efficiencytable 60, to look up and/or define the value for the oxidation catalystdiffusion efficiency ratio 58, which is the output of the diffusionefficiency table 60.

As shown in FIG. 3, once the oxidation catalyst diffusion efficiencyratio 58 is obtained from the diffusion efficiency table 60, and thesecond intermediate variable for hydrocarbon oxidation 56 (ζ_(O2)) iscalculated from Equation 5, the first intermediate variable forhydrocarbon oxidation 54 may be calculated by dividing, generallyindicated by box 66, the second intermediate variable for hydrocarbonoxidation 56 by the oxidation catalyst diffusion efficiency ratio 58.The first intermediate variable for hydrocarbon oxidation 54 and thetemperature of the catalytic device 38 (T) are then used as the inputsinto the burn efficiency table 50 to obtain the oxygen burn efficiencyratio 46. The oxygen burn efficiency ratio 46 is then multiplied,generally indicated by box 68, by the amount of O2 available forreaction with hydrocarbons per unit volume of exhaust gas 48, to defineand/or calculate the O2 consumed in the catalytic device per unit volumeof exhaust gas 44 (Δ[O2]).

Referring to FIG. 4, the amount of hydrocarbons absorbed in thecatalytic device per unit volume of exhaust gas 72 (Δ[HC]_(absorp)) is afunction of a hydrocarbon absorption efficiency ratio 74, and ahydrocarbon concentration available for absorption 76. The hydrocarbonconcentration available for absorption 76 is calculated from Equation 6:

$\begin{matrix}{{{{\eta \;}_{diff}\left( \frac{\lbrack{HC}\rbrack_{in} + {\lbrack{HC}\rbrack_{- 1}\frac{t_{res}}{\Delta \; t}}}{1 + \frac{t_{res}}{\Delta \; t}} \right)} + {\left( \frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}} \right)\Omega \; k_{desorp}}};} & \left. 6 \right)\end{matrix}$

wherein η_(diff) is the oxidation catalyst diffusion efficiency ratio,[HC]_(in) is an oxidation catalyst inlet hydrocarbon concentration,[HC]⁻¹ is the hydrocarbon concentration in the catalytic device at thelast time increment, t_(res) is the residence time of the exhaust gaswithin the catalytic device, Δt is the change in time (i.e., timeduration), Ω is the maximum amount of hydrocarbon storage per unitvolume of the catalytic device, and k_(desorp) is the normalizedhydrocarbon storage desorption rate.

As shown in FIG. 4, a value for the hydrocarbon absorption efficiencyratio 74 may be obtained from an absorption efficiency table 78, storedin the memory of the controller. Obtaining the value, generallyindicated by box 80, for the hydrocarbon absorption efficiency ratio 74,which is used to calculate the amount of hydrocarbons absorbed in thecatalytic device per unit volume of exhaust gas 72 (Δ[HC]_(absorp)), mayinclude referencing the absorption efficiency table 78 to look-up thevalue for the hydrocarbon absorption efficiency ratio 74. The absorptionefficiency table 78 may be defined as a two dimensional table, that usestwo input values to define an output value. The hydrocarbon absorptionefficiency ratio 74 is based upon a temperature of the catalytic device38 (T), and a first intermediate variable for hydrocarbon absorption 82.Accordingly, the controller may use the temperature of the catalyticdevice 38 (T) and the first intermediate variable for hydrocarbonabsorption 82 as the two inputs into the absorption efficiency table 78,to look up and/or define the value for the hydrocarbon absorptionefficiency ratio 74, which is the output of the absorption efficiencytable 78.

As shown in FIG. 4, the first intermediate variable for hydrocarbonabsorption 82 is a function of a second intermediate variable forhydrocarbon absorption 84 (ζ_(HC) _(—) _(absorp)), and the oxidationcatalyst diffusion efficiency ratio 58. The second intermediate variablefor hydrocarbon absorption 84 (ζ_(HC) _(—) _(absorp)) may be calculatedfrom Equation 7:

$\begin{matrix}{{{\varsigma \; {HC\_ absorp}} = {{\Omega \left( {1 - \theta_{HC}} \right)}\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}};} & \left. 7 \right)\end{matrix}$

wherein Ω is the maximum amount of hydrocarbon storage per unit volumeof the catalytic device, θ_(HC) is the normalized hydrocarbon storage ofthe catalytic device, t_(res) is the residence time of the exhaust gaswithin the catalytic device, and Δt is the change in time (i.e., timeduration).

As shown in FIG. 4, a value for the oxidation catalyst diffusionefficiency ratio 58 may be obtained from the diffusion efficiency table60, stored in the memory of the controller. Obtaining the value,generally indicated by box 86, for the oxidation catalyst diffusionefficiency ratio 58, which is used to calculate the first intermediatevariable for hydrocarbon oxidation 82, may include referencing thediffusion efficiency table 60 to look-up the value for the oxidationcatalyst diffusion efficiency ratio 58. The diffusion efficiency table60 may be defined as a one dimensional table that uses one input valueto define a single output value. The oxidation catalyst diffusionefficiency ratio 58 is based upon the residence time of the exhaust gaswithin the catalytic device 64 (t_(res)). Accordingly, the controllermay use the residence time of the exhaust gas within the catalyticdevice 64 (t_(res)) as the single input into the diffusion efficiencytable 60, to look up and/or define the value for the oxidation catalystdiffusion efficiency ratio 58, which is the output of the diffusionefficiency table 60.

As shown in FIG. 4, once the oxidation catalyst diffusion efficiencyratio 58 is obtained from the diffusion efficiency table 60, and thesecond intermediate variable for hydrocarbon absorption 84 (ζ_(HC) _(—)_(absorp)) is calculated from Equation 7, the first intermediatevariable for hydrocarbon absorption 82 may be calculated by dividing,generally indicated by box 88, the second intermediate variable forhydrocarbon absorption 84 (ζ_(HC) _(—) _(absorp)) by the oxidationcatalyst diffusion efficiency ratio 58. The first intermediate variablefor hydrocarbon absorption 82 and the temperature of the catalyticdevice 38 (T) are then used as the inputs into the absorption efficiencytable 78 to obtain the hydrocarbon absorption efficiency ratio 74. Thehydrocarbon absorption efficiency ratio 74 is then multiplied, generallyindicated by box 90, by the hydrocarbon concentration available forabsorption 76, to define and/or calculate the amount of hydrocarbonsabsorbed in the catalytic device per unit volume of exhaust gas 72(Δ[HC]_(absorp)).

The operation of the vehicle may be controlled based upon the estimatedhydrocarbon storage of the catalytic device. For example, the engine maybe controlled to heat the catalyst to the light-off temperature, toregenerate the catalytic device(s), or fuel may be injected into theflow of exhaust gas for combustion to further heat the catalyst.

The detailed description and the drawings or figures are supportive anddescriptive of the invention, but the scope of the invention is definedsolely by the claims. While some of the best modes and other embodimentsfor carrying out the claimed invention have been described in detail,various alternative designs and embodiments exist for practicing theinvention defined in the appended claims.

1. A method of estimating hydrocarbon storage in a catalytic device of an exhaust gas treatment system, the method comprising: determining hydrocarbon absorption by the catalytic device over a period of time, hydrocarbon desorption by the catalytic device over the period of time, and hydrocarbon oxidation in the catalytic device over the period of time; estimating the hydrocarbon storage of the catalytic device, with a controller, from the equation: ${\Omega \frac{\theta_{HC}}{t}} = \frac{{\Delta \lbrack{HC}\rbrack}_{absorp} - {\Delta \lbrack{HC}\rbrack}_{desorp} - {\Delta \lbrack{HC}\rbrack}_{oxi}}{\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}$ wherein $\Omega \frac{\theta_{HC}}{t}$  is the rate of change in hydrocarbon storage per unit volume of the catalytic device, Δ[HC]_(absorp) is the amount of hydrocarbons absorbed in the catalytic device per unit volume of exhaust gas, Δ[HC]_(desorp) is the amount of hydrocarbons desorbed in the catalytic device per unit volume of exhaust gas, Δ[HC]_(oxi) is the amount of hydrocarbons oxidized in the catalytic device per unit volume of exhaust gas, t_(res) is the residence time of the exhaust gas within the catalytic device, and Δt is the change in time (i.e., time duration); and controlling the exhaust gas treatment system based upon the estimated hydrocarbon storage of the catalytic device.
 2. The method set forth in claim 1 wherein Δ[HC]_(desorp) is calculated from the equation: ${\Delta \lbrack{HC}\rbrack}_{desorp} = {\left( \frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}} \right)\Omega \; k_{desorp}}$ wherein t_(res) is the residence time of the exhaust gas within the catalytic device, Δt is the change in time (i.e., time duration), Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, and k_(desorp) is the normalized hydrocarbon storage desorption rate.
 3. The method set forth in claim 2 further comprising obtaining a value for k_(desorp) from a table based upon a temperature of the catalytic device (T) and a normalized hydrocarbon storage of the catalytic device (θ_(HC)).
 4. The method set forth in claim 1 wherein Δ[HC]_(oxi) is calculated from the equation: ${\Delta \lbrack{HC}\rbrack}_{oxi} = \frac{\Delta \left\lbrack {O\; 2} \right\rbrack}{{Ratio}_{{stoic\_ O}\; 2{\_ HC}}}$ wherein Δ[O2] is the O2 (oxygen) consumed in the catalytic device per unit volume of exhaust gas, and Ratio_(stoic) _(—) _(O2) _(—) _(HC) is the O2 and hydrocarbon reaction stoichiometric ratio.
 5. The method set forth in claim 4 wherein the O2 consumed in the catalytic device per unit volume of exhaust gas (Δ[O2]) is a function of an oxygen burn efficiency ratio and an amount of O2 available for reaction with hydrocarbons per unit volume of exhaust gas, wherein the amount of O2 available for reaction with hydrocarbons per unit volume of exhaust gas is calculated from the equation: $\eta_{diff}\left( \frac{\left\lbrack {O\; 2} \right\rbrack_{in} + {\left\lbrack {O\; 2} \right\rbrack_{- 1}\frac{t_{res}}{\Delta \; t}}}{1 + \frac{t_{res}}{\Delta \; t}} \right)$ wherein η_(diff) is the oxidation catalyst diffusion efficiency ratio, [O2]_(in) is the oxidation catalyst inlet O2 concentration, [O2]⁻¹ is the O2 concentration in the catalytic device at last time increment, t_(res) is the residence time of the exhaust gas within the catalytic device, and Δt is the change in time (i.e., time duration).
 6. The method as set forth in claim 5 further comprising obtaining a value for the oxygen burn efficiency ratio from a table based upon a temperature of the catalytic device (T) and a first intermediate variable for hydrocarbon oxidation.
 7. The method as set forth in claim 6 wherein the first intermediate variable for hydrocarbon oxidation is a function of a second intermediate variable for hydrocarbon oxidation (ζ_(O2)) and a oxidation catalyst diffusion efficiency ratio; wherein ζ_(O2) is calculated from the equation: ${\varsigma \; O\; 2} = {\Omega \; {f\left( \theta_{HC} \right)}\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}$ wherein Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, ƒ(θ_(HC)) is a function of the normalized hydrocarbon storage of the catalytic device, t_(res) is the residence time of the exhaust gas within the catalytic device, and Δt is the change in time (i.e., time duration).
 8. The method set forth in claim 7 further comprising obtaining a value of the oxidation catalyst diffusion efficiency ratio from a table based upon the residence time of the exhaust gas within the catalytic device (t_(res)).
 9. The method set forth in claim 1 wherein Δ[HC]_(absorp) is a function of a hydrocarbon absorption efficiency ratio and a hydrocarbon concentration available for absorption, wherein the hydrocarbon concentration available for absorption is calculated from the equation: ${{\eta \;}_{diff}\left( \frac{\lbrack{HC}\rbrack_{in} + {\lbrack{HC}\rbrack_{- 1}\frac{t_{res}}{\Delta \; t}}}{1 + \frac{t_{res}}{\Delta \; t}} \right)} + {\left( \frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}} \right)\Omega \; k_{desorp}}$ wherein η_(diff) is the oxidation catalyst diffusion efficiency ratio, [HC]_(in) oxidation catalyst inlet hydrocarbon concentration, [HC]⁻¹ is the hydrocarbon concentration in the catalytic device at the last time increment, t_(res) is the residence time of the exhaust gas within the catalytic device, Δt is the change in time (i.e., time duration), Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, and k_(desorp) is the normalized hydrocarbon storage desorption rate.
 10. The method as set forth in claim 9 further comprising obtaining a value for the hydrocarbon absorption efficiency ratio from a table based upon the temperature of the catalytic device (T) and a first intermediate variable for hydrocarbon absorption.
 11. The method as set forth in claim 10 wherein the first intermediate variable for hydrocarbon absorption is a function of a second intermediate variable for hydrocarbon absorption (ζ_(HC) _(—) _(absorp)) and a oxidation catalyst diffusion efficiency ratio, wherein ζ_(HC) _(—) _(absorp) is calculated from the equation: ${\varsigma \; {HC\_ absorp}} = {{\Omega \left( {1 - \theta_{HC}} \right)}\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}$ wherein Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, θ_(HC) is the normalized hydrocarbon storage of the catalytic device, t_(res) is the residence time of the exhaust gas within the catalytic device, and Δt is the change in time (i.e., time duration).
 12. The method set forth in claim 10 further comprising obtaining a value of the oxidation catalyst diffusion efficiency ratio from a table based upon the residence time of the exhaust gas within the catalytic device (t_(res)).
 13. The method set forth in claim 1 further comprising providing a controller, including all necessary hardware, software, algorithms, sensors, and memory necessary to estimate the hydrocarbon storage in the catalytic device.
 14. A method of estimating hydrocarbon storage in a catalytic device of an exhaust gas treatment system, the method comprising: calculating, with a controller, an amount of hydrocarbons absorbed in the catalytic device per unit volume of exhaust gas over a period of time; calculating, with the controller, an amount of hydrocarbons desorbed in the catalytic device per unit volume of exhaust gas over the period of time; calculating, with the controller, an amount of hydrocarbons oxidized in the catalytic device per unit volume of exhaust gas over the period of time; subtracting, with the controller, the amount of hydrocarbons oxidized in the catalytic device and the amount of hydrocarbons desorbed in the catalytic device from the amount of hydrocarbons absorbed in the catalytic device to determine the amount of hydrocarbons stored in the catalytic device; and controlling the exhaust gas treatment system based upon the estimated hydrocarbon storage of the catalytic device.
 15. The method set forth in claim 14 further comprising providing a controller, including all necessary hardware, software, algorithms, sensors, and memory necessary to determine the amount of hydrocarbons stored in the catalytic device.
 16. The method set forth in claim 15 wherein calculating the amount of hydrocarbons desorbed in the catalytic device is further defined as calculating the amount of hydrocarbons desorbed in the catalytic device from the equation Δ[HC]_(desorp) is calculated from the equation: $\left( \frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}} \right)\Omega \; k_{desorp}$ wherein t_(res) is the residence time of the exhaust gas within the catalytic device, Δt is the change in time (i.e., time duration), Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, and k_(desorp) is the normalized hydrocarbon storage desorption rate.
 17. The method set forth in claim 15 wherein calculating the amount of hydrocarbons oxidized in the catalytic device is further defined as calculating the amount of hydrocarbons oxidized in the catalytic device from the equation: $\frac{\Delta \left\lbrack {O\; 2} \right\rbrack}{{Ratio}_{{stoic\_ O}\mspace{11mu} 2{\_ HC}}}$ wherein Δ[O2] is the O2 (oxygen) consumed in the catalytic device per unit volume of exhaust gas, and Ratio_(stoic) _(—) _(O2) _(—) _(HC) is the O2 and hydrocarbon reaction stoichiometric ratio.
 18. The method set forth in claim 15 wherein calculating the amount of hydrocarbons absorbed in the catalytic device is a function of a hydrocarbon absorption efficiency ratio and a hydrocarbon concentration available for absorption, wherein the hydrocarbon concentration available for absorption is calculated from the equation: ${{\eta \;}_{diff}\left( \frac{\lbrack{HC}\rbrack_{in} + {\lbrack{HC}\rbrack_{- 1}\frac{t_{res}}{\Delta \; t}}}{1 + \frac{t_{res}}{\Delta \; t}} \right)} + {\left( \frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}} \right)\Omega \; k_{desorp}}$ wherein η_(diff) is the oxidation catalyst diffusion efficiency ratio, [HC]_(in) oxidation catalyst inlet hydrocarbon concentration, [HC]⁻¹ is the hydrocarbon concentration in the catalytic device at the last time increment, t_(res) is the residence time of the exhaust gas within the catalytic device, Δt is the change in time (i.e., time duration), Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, and k_(desorp) is the normalized hydrocarbon storage desorption rate.
 19. The method as set forth in claim 18 further comprising obtaining a value for the hydrocarbon absorption efficiency ratio from a table based upon the temperature of the catalytic device (T) and a first intermediate variable for hydrocarbon absorption; wherein the first intermediate variable for hydrocarbon absorption is a function of a second intermediate variable for hydrocarbon absorption (ζ_(HC) _(—) _(absorp)) and a oxidation catalyst diffusion efficiency ratio; wherein ζ_(HC) _(—) _(absorp) is calculated from the equation: ${\varsigma \; {HC\_ absorp}} = {{\Omega \left( {1 - \theta_{HC}} \right)}\frac{t_{res}}{1 + \frac{t_{res}}{\Delta \; t}}}$ wherein Ω is the maximum amount of hydrocarbon storage per unit volume of the catalytic device, θ_(HC) is the normalized hydrocarbon storage of the catalytic device, t_(res) is the residence time of the exhaust gas within the catalytic device, and Δt is the change in time (i.e., time duration).
 20. The method set forth in claim 19 further comprising obtaining a value of the oxidation catalyst diffusion efficiency ratio from a table based upon the residence time of the exhaust gas within the catalytic device (t_(res)). 